CN1330696A - Integration of solvent deasphalting and gasification - Google Patents
Integration of solvent deasphalting and gasification Download PDFInfo
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- CN1330696A CN1330696A CN99810542A CN99810542A CN1330696A CN 1330696 A CN1330696 A CN 1330696A CN 99810542 A CN99810542 A CN 99810542A CN 99810542 A CN99810542 A CN 99810542A CN 1330696 A CN1330696 A CN 1330696A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S208/00—Mineral oils: processes and products
- Y10S208/95—Processing of "fischer-tropsch" crude
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention is the integration of a process of gasifying asphaltenes in a gasification zone by partial oxidation and the process of asphaltene extraction with a solvent. The integration allows low level heat from the gasification reaction to be utilized in the recovery of solvent that was used to extract asphaltenes from an asphaltene-containing hydrocarbon material. Asphaltenes are extracted from an asphaltene-containing hydrocarbon material by mixing a solvent in quantities sufficient to precipitate at least a fraction of the asphaltenes. The precipitated asphaltenes are then gasified in a gasification zone to synthesis gas. The gasification process is very exothermic. The low level heat in the synthesis gas, either directly, or via an intermediate step of low pressure steam, is used to remove and recover the solvent from the deasphalted hydrocarbon material and from the asphaltenes prior to gasification.
Description
Invention field
The present invention relates to a kind of from oil, heavy oil, decompression or distillation residue the extraction and the bitum technology that gasifies.More particularly, the present invention relates to the process integration of gasifying process and diasphaltene technology, this technology can be utilized the used heat (being used heat in other cases) of gasifying process and the bituminous matter of low value can be transformed into the synthetic gas of high value.
Background of invention
Many crude oil contain a large amount of bituminous matters.Wish and the bituminous matter in the oil can be removed that this is because processing units subsequently will be solidified and stop up to bituminous matter, also can reduce oil viscosity because remove bituminous matter.Bituminous matter solvent extraction process residual oils is generated deasphalted oil (DA0),, mainly generate diesel oil then with the deasphalted oil catalytic cracking.Common diasphaltene technology comprises heavy oil is contacted with solvent.Solvent generally is that alkane such as propane are to pentane.The solvability of solvent in heavy oil reduces with the rising of temperature.The temperature of selecting is that all basically alkane is all dissolved, and a part of resin and asphaltene precipitation.Because the solubleness of bituminous matter in this solvent-oil mixt is low, so asphaltene precipitation and from oil, separating.
Then, generally arrive sufficiently high temperature with high pressure steam or fired heater heating deasphalted oil-solvent mixture.Then need not just can be with oil and separated from solvent with solvent evaporation.This is with respect to reducing the about 20-30% of energy waste with separated from solvent, being recycled.
Choice of Solvent depends on the quality of oil.When the molecular weight of solvent increased, the requirement of solvent reduced, but selectivity reduces as the selectivity to resin and aromatics.Propane needs more solvent but can not extract with aromatics and the resin measured.With than the solvent of small molecular weight the time, the expense of solvent recuperation is generally than higher.
With hydrocarbons be gasificated into the technology of synthetic gas and advantage industrial be known.The hydrocarbons that has gasified comprises solid, liquid and composition thereof.Gasification comprises mixes a certain amount of oxygen-containing gas under certain conditions, to be enough to the making hydrocarbons partial oxygen change into carbon monoxide and hydrogen.Gasification is emitted a large amount of heat.Gas temperature in the gasifying reactor usually is higher than 1100 ℃ (2000 °F).Usually the synthetic gas of water quenching heat is produced steam with a part of remaining sensible heat in the gas then.Arriving certain temperature just can not regeneration steam.Then, the waste heat in the gas generally just is discharged in the atmosphere by fan cooler.
Summary of the invention
The present invention be in the gasification zone by partial oxidation to gasify bitum technology and with the process integration of the bitum technology of solvent extraction.This process integration makes the low level heat (low level heat) from gasification reaction can be used in recovery and extract the solvent that bituminous matter is used from the hydrocarbons of asphaltenes.The extraction bituminous matter is to make at least a portion asphaltene precipitation by mixing sufficient amount of solvent from the hydrocarbons of asphaltenes.Use any traditional method with precipitated asphalt matter and alkane separating substances then.There is no need to make the alkane material to separate with precipitated asphalt matter fully.A spot of alkane material can gasify together with bituminous matter.But, do not wish the alkane gasification substance, because it is more valuable as catalytically cracked material.
Make precipitated asphalt matter be gasificated into synthetic gas then in the gasification zone.Gasification is emitted a large amount of heat, and the synthetic gas that leaves the gasification zone is very warm.Usually with heat exchanger with synthetic gas quenching and cooling, it is favourable producing steam therein.Can generate high pressure (or high quality) steam and low pressure (or inferior quality) steam in succession.But when the temperature of synthetic gas reduced, the quality of steam reduced, when temperature is reduced to certain value, and just can not regeneration steam.
Can directly or by the intermediate steps of low-pressure steam come from alkane material (being also referred to as deasphalted oil (DAO)), to remove and reclaim solvent with the low level heat in the synthetic gas.Low level heat also can advantageously be used for removing the solvent in precipitation and the isolating bituminous matter before gasification, particularly (in slurries) during the hydrocarbons after a large amount of diasphaltenes are arranged in the bituminous matter.
Description of drawings
Fig. 1 illustrates the different embodiment of the present invention with Fig. 2.
Detailed Description Of The Invention
In the application's context, term used in the asphaltene precipitation " precipitation " is referred to be rich in bitum material to form second phase, can be and preferably fluid or similar fluidic phase.In a preferred embodiment of the invention, sedimentaryly be rich in bitum substance pump to gasifier.Because handle problems, it is not preferred mutually that solid is rich in bitum.
Used term " gasification zone " refers to and makes the hydrocarbons that enters particularly be rich in bitum material in the reactor to mix with oxygen-containing gas and carry out partially combusted zone among the application.
Used term " hydrocarbons after the diasphaltene " among the application, " deasphalted oil ", DAO and " paraffin oil " are used interchangeably, and refer to the oil in the deasphalting solvent that can be dissolved in selection under the condition that the diasphaltene operation is selected.
The present invention is the process integration of the technology that gasifies with the bitum technology of solvent extraction with by partial oxidation, the used solvent of recovery of heat extraction bituminous matter that it utilizes gasification to produce.Combination can be transformed into valuable synthetic gas with usual nugatory byproduct bituminous matter with solvent deasphalting by gasifying.
This technology is applicable to the hydrocarbons of asphaltenes.This material is fluid such as oil or heavy oil normally.In the refinery that produces the light hydrocarbon oil cut, carry out on a large scale usually accessing residual oil in the still-process of crude oil.This technology also is applicable to this residual oil.The hydrocarbons of asphaltenes even can look like it is solid is particularly under usual conditions.The hydrocarbons of this asphaltenes should be that part is miscible with solvent at least under extraction temperature.
It is known extracting bituminous matter with lower boiling solvent from the hydrocarbons of asphaltenes.For example, referring to United States Patent (USP) 4391701 and 3617481, introduce these patents herein as a reference.Deasphalting step is included in the hydrocarbons of solvent and asphaltenes is contacted.It is favourable keeping temperature and pressure, and can make the hydrocarbons of asphaltenes and lower boiling solvent like this is fluid or class quasi-fluid.Can add some additive in order to improve deasphalting efficient, these additives comprise light oil, aromatic series washing oil, mineral acid etc.Their contact can be passed through intermittent mode, and successive fluid-fluid countercurrent current mode or any alternate manner well known in the art carry out.Bituminous matter forms crystal, can utilize gravity separation, filters, and centrifugation or any alternate manner well known in the art make it separate with hydrocarbons after the diasphaltene.
Quality with the hydrocarbons after metal content and the diasphaltene that sulphur content is represented becomes inverse change with the amount of isolated bituminous matter and resin.For example, removing in deoiling the bituminous matter of 30wt%, that heavy metal is reduced is about 90%, still, removes that the bituminous matter of 10wt% may make heavy metal only reduce about 60% in deoiling.The bitum amount of removing and gasifying preferably asphaltenes hydrocarbons at least about 20wt%, more preferably be about 30wt% at least.
Solvent can be any suitable deasphalting solvent.Being generally used for deasphalting solvent is the compound that light aliphatic hydrocrbon promptly has 2-8 carbon atom.Alkane particularly contains propane, and butane, the solvent of pentane or its mixture are suitable in the present invention.Concrete preferred solvent depends on bitum specific nature.Be applicable to the bituminous matter of higher pitch ring and ball softening point than heavy solvent.What solvent can contain less share promptly is lower than about 20% higher alkane such as hexane or heptane.
Most of deasphalting solvents are round-robin, so it contains light hydrocarbon mixture usually.Preferred solvent is the alkane that 3-5 carbon atom arranged, and promptly contains the propane of 80wt% at least, butane, the solvent of pentane or its mixture.Because (evaporation) solvent uses is relatively low temperature in extraction the hydrocarbons after diasphaltene, so most preferred solvent contains propane and the butane of 80wt% at least, or butane and the pentane of 80wt% at least.
The gasification of heavy oil and hydrocarbonaceous solid comprises that with hydrocarbonaceous material be bituminous matter and randomly, and other hydrocarbonaceous material and oxygen-containing gas mix in the gasification zone, and condition wherein is to make oxygen and hydrocarbonaceous material reaction form synthetic gas.Can make heavy oil or solid be transformed into synthetic gas by gasification, this is a value product.Composition hydrogen in the synthetic gas and carbon monoxide are recyclable to sell or to be used in the refinery.For example, synthetic gas can be used as fuel with instead of natural gas, or as the precursor of various chemical substances such as methyl alcohol.
It also is known utilizing the sensible heat generation steam in the hot synthesis gas.For example, referring to United States Patent (USP) 4597773, introduce this patent herein as a reference.The used term " sensible heat " of the application is the energy that gas is emitted when being cooled to another temperature by a temperature.Therefore, if in fact condensation really of any component in the gas, then sensible heat comprises the heat of condensation of component.After generating steam, the low mass-energy (low quality energy) of a large amount of sensible heat forms is arranged in the synthetic gas.Extracting heat energy production high pressure steam from synthetic gas can be with gas cooling to about 260 ℃.Further the production low-pressure steam can be with gas cooling to about 170 ℃.Remaining sensible heat is usually discharged into the atmosphere by fan cooler in the synthetic gas.The process integration of diasphaltene and gasification provides a kind of beneficial method of utilizing this energy.
Bituminous matter in the oil makes the way far away transportation of oil and processing become difficult.In order to make the value maximization of non-refinable crude lubricating oil, the separation of the asphalt component in the oil is carried out for many years.Reclaiming the non-asphaltene component sells and the bituminous matter component of remaining no much value as value product.Bituminous matter is the hydrocarbonaceous material that is fit to gasification.For example, referring to United States Patent (USP) 4391701, introduce this patent herein as a reference.
The process integration of solvent deasphalting technology and gasifying process makes the useful especially utilization of process heat become possibility.The a large amount of heat of solvent deasphalting arts demand with reclaim and cycling extraction pitch in used solvent.The solvent that goes out in light oil and the pitch logistics with hot stripping enables to reclaim and turn back in this technology.In traditional deasphalting unit, usually use fired heater or produce the necessary heat of diasphaltene technology from the high pressure steam of generator.When the logistics the hot heated solvent deasphalting unit of process that utilization can obtain from gasifier, the fund of solvent deasphalting and running cost will reduce.The heat that needs reduces, and the fuel that consumes seldom heats this process-stream.
Gasification is heat release.Available sensible heat is produced high pressure (greater than 600psi or 4140KPa) steam and low pressure (100-200psi, or about 700-1380KPa) steam.The applicant finds by utilize the solvent in the hydrocarbons of producing after the energy that reclaims behind the steam reclaims diasphaltene from low-pressure steam and synthetic gas, can effectively utilize the sensible heat in the synthetic gas rather than make it waste by fan cooler.The temperature of the synthetic gas after production high quality or the high pressure steam is higher than about 260 ℃.This heat can directly be used for separating the solvent in the hydrocarbons after the diasphaltene.Further the production low-pressure steam can be with gas cooling to about 170 ℃.Produce the sensible heat in the synthetic gas behind the low-quality steam and be used to provide the heat of the solvent in the hydrocarbons that separates after the diasphaltene.Low-quality steam can advantageously be used for finishing removes and reclaims solvent.
Also can be with the mixture pressurization of the hydrocarbons after solvent and the diasphaltene, the downstream of bituminous matter extraction allows that multiple-effect evaporation is had enough impellents.Flash distillation can be carried out under different temperature, can advantageously add low potential energy at evaporation stage at least.
Being different from as the solvent deasphalting technology of a part of the present invention can other commercial technology.In the process integration of solvent deasphalting and gasification, deasphalting unit makes from the utilization maximization of the low level heat of synthetic gas and does not use a large amount of high quality steam or naked light well heater.This does not just need with the solvent among the naked light well heater recovery DAO.
Make the hydrocarbons after the diasphaltene and the mixture of solvent be exposed to low-qualityer heat (lower quality heat), this heat can be from the synthetic gas behind the production inferior quality steam, and the synthetic gas that can advantageously be exposed to sometimes after low-pressure steam or the production high pressure steam just is enough to and will separates the hydrocarbons of most solvent after diasphaltene.With the overcritical crystallization of high temperature be separated on the contrary, comprise evaporation, separate and the separating step that reclaims solvent can utilize vacuum.But, be more typically with steam extraction and remove and to desolvate so the solvent of strips residual effectively.
The low potential energy preheating material that also can advantageously be used to autopneumatolysis is to be fed to deasphalted oil stripping tower and pitch stripping tower.The hot preheating of process that produces with gasification unit can make the load and/or the high pressure steam amount of separating the required fired heater of solvent minimize.
Total used heat may Duo about 20% to about 40% with high pressure steam or combustion chamber and the used heat of supercritical extraction than traditional.But the improvement that this technology is great is that this low-quality heat is used heat, also is to utilize this heat usually can save and uses at least one fan cooler.
Usually the process heat of producing in gasifier that is sent to fan cooler is used for heating the process-stream of deasphalting unit, that is: feed stream, deasphalting unit itself and product stream.Therefore, utilize the Lowlevel thermal energy in the gasifier enough to reduce the cost of gasifier, because save fund cost expense and running cost that fan cooler can reduce gasifier.Because low potential energy is hunted down and is used in the deasphalting unit, so the efficient of gasifier also can improve.
In solvent deasphalting technology, be the raw material of valuable catalytic cracking with liquid-liquid extraction method hydrocarbons after the isolated diasphaltene from the hydrocarbons of asphaltenes.On the other hand, the isolating value that is rich in bitum material is much lower, is the ideal gasified raw material therefore.Raw material with liquid-liquid extraction method isolated catalytic cracking from the hydrocarbons of asphaltenes is many more, and bitum viscosity is big more.Past, but in order in being rich in bitum material, to stay abundant oil so that be rich in bitum material pumping, just reduce the productive rate of deasphalting unit.The productive rate that reduces the raw material of valuable catalytic cracking in order to keep bitum viscosity will make this unitary profit reduce.
Bituminous matter is retained in the hydrocarbons after the diasphaltene as pumpable fluid or slurries can be easy to solve the problem relevant usually with bituminous matter.But, from raw materials technology that separated from solvent and recovery is normally favourable.It also is favourable that the amount of the hydrocarbons after the diasphaltene of being sent to gasifier is minimized, that is, preferably at least about the hydrocarbons after the diasphaltene of 90wt% and precipitated asphalt pledge flow point from.
In one embodiment of the invention, be rich in bitum material from solvent stripping tower bottom directly pump to gasifier.The bitum material that is rich in of stripping tower bottom is hot, and promptly about 170 ℃ to about 260 ℃, the viscosity of this material reduces when high temperature.Therefore, the extremely heavy bitum material of producing from the high yield operation (wherein isolating the raw material of the valuable catalytic cracking of very high percentage amounts) that is rich in remains pumpable.Keeping this gasifier raw material is very favourable as pumpable fluid.
In this embodiment, the residue of deasphalting unit comprises and is rich in bitum material, and some residual solvents and small portion of residual paraffin oil should the bottom heating before logistics is sent to the solvent stripping tower.When still existing, solvent can more effectively heat bituminous matter.Bitum heat conductivity is low, and bitum under many circumstances viscosity makes it effectively not mix.The easier heat absorption of solvent.When solvent existed, the viscosity that is rich in bitum material was lower.This just makes that heat distributes more effectively in being rich in bitum material.Therefore, heating the mixture that is rich in bitum material and solvent can be more effective than only heating bituminous matter.
When solvent when stripping goes out from be rich in bitum material, be rich in bitum material in the residue and still be in high temperature.In this time period, can increase heat to keep high temperature.Keep high temperature can make bituminous matter that lower viscosity is arranged and make that to be rich in bitum material be pumpable.This helps being rich in the conveying of bitum material to gasifier.Advantageously, the fresh feed pump of gasification unit places the bottom of stripping tower.
Gasifier receives heat pumpablely is rich in bitum raw material.The high temperature raw material has improved the processing property of gasifier, because raw material can more effectively atomize.Next this can cause more effective reaction kinetics.
In this embodiment, importantly make and be rich in bitum material and keep high temperature.Because bitum heat conductivity is low, so solvent recuperation post-heating bituminous matter is very difficult to reach the viscosity requirement.Therefore, advantageously make carry be rich in bitum material to the pipe insulation of gasifier so that be rich in the cooling of bitum material during carrying and minimize, when technology is interrupted, can use the material such as the heavy oil of additional heating installation or pipe blow-through (line-purge).
The structure of this embodiment of the present invention also is favourable, because the operating equipment of stripping tower is as the feed drum of gasifier.Bituminous matter is not easy to fluid storage.Be rich in bitum material cooling if make, it will become can not pumping and final curing.For the smooth running gasifier, need feed drum.Before operation, use this charger recycle feed between the starting period, use this charger to absorb the delivery rate fluctuation, during closing deasphalting unit, use this charger to make gasifier keep operation can be sent to this unit up to another batch raw material at normal operation period.
Other hydrocarbonaceous material in other source can gasify together with bituminous matter.For example, useless hydrocarbon, heavy oil, coal and tar can gasify together with bituminous matter.If make that because the adding of these other materials can not form pumpable material these other materials can not be when being rich in bitum material and mixing, it is useful that these additional raw materials are injected into gasifier separately.
Isolating solvent the hydrocarbon material flow after diasphaltene, if feasible from isolating or the isolating bituminous matter logistics of part isolating solvent, be recycled and utilize again that to make the hydrocarbons diasphaltene of more asphaltenes be favourable.Recovered solvent may need to handle the compound that promptly contains 5-10 carbon atom with the hydrocarbon that removes gasoline-range, it be when the stripping solvent the hydrocarbons after diasphaltene stripping come out.The hydrocarbon of said gasoline-range can mix to reduce the viscosity of this material with the hydrocarbons after the diasphaltene, perhaps makes the hydrocarbon of gasoline-range can be used as independent product treatment.If the amount of the hydrocarbon of gasoline-range is less than usually with more heat and separates and reclaim the amount of extracting under the situation of solvent.Another kind of mode is, the material by making asphaltenes with solvent before underpressure distillation the amount of said hydrocarbon is minimized.
Also have other technology such as desalinating process, consider the viscosity of the heavy oil that the present invention uses usually, this technology is useful after heavy oil and solvent.
Fig. 1 is the synoptic diagram of one embodiment of the invention.The hydrocarbons of asphaltenes enters normal pressure or decompression separation chamber 10 by pipeline 12.This material can be the (not shown) of heating.Light oil separates from the hydrocarbons of asphaltenes and 10 discharges from the separate chamber by pipeline 14.The hydrocarbons of asphaltenes leaves normal pressure or the decompression separation chamber enters bituminous matter extractor 20 by pipeline 16.Solvent enters bituminous matter extractor (20) by pipeline 82 from solvent condenser (80).Hydrocarbons after bituminous matter and some diasphaltenes leaves bituminous matter extractor (20) by pipeline 22.This logistics in the water back 22 also reclaims solvent as described.Be rich in the preheating in heat exchanger 86 of bitum material, then by pipeline 88 input solvent stripping towers.In this embodiment, the low-pressure steam from pipeline 84 is used as thermal source.Alternatively use high pressure steam, synthetic gas or series of heat interchanger.The bitum material that is rich in of heat is transported to solvent stripping tower 90 by pipeline 88.In this embodiment, the high pressure steam from pipeline 44 that produces by cooling syngas is used for the stripping solvent.This all high pressure steam of may not can using up, 96 expressions of pipeline are discharged some steam to use it for anything else, for example the solvent in the stripping paraffin oil.The bituminous matter of heat pumps into gasifier 30 by pipeline 94.Logistics in the pipeline 94 enters gasification zone 30, and it mixes with the oxygen-containing gas that imports by pipeline 32 there.The very hot synthetic gas that the partial oxidation that carries out in the gasification zone 30 produces leaves the gasification zone by pipeline 34.Part cooling gas and the water quench system of removing particle do not illustrate.The synthetic air of heat is through heat exchanger 40, and wherein the water in the pipeline 42 is transformed into high-quality steam in the pipeline 44.This steam is to be used in diasphaltene technology or other local product.Synthetic gas leaves heat exchanger 40 by pipeline 46 and enters second heat exchanger 50 then.The synthetic air of heat is through heat exchanger 50, and wherein the water in the pipeline 52 is transformed into low-quality steam in the pipeline 54.Synthetic gas leaves heat exchanger 50 then.Remaining sensible heat can provide the extra low level heat of arts demand in the synthetic gas.An embodiment is sent to the heat exchanger that interrelates with separator column 60 with synthetic gas.This synthetic gas is only as process warm.It not with deasphalted oil, solvent or bituminous matter are mixed.Also enter separator column 60 from the hydrocarbons after the diasphaltene of bituminous matter extractor 20 (being also referred to as paraffin) by pipeline 24.By the synthetic gas with heat, steam or the two are all as thermal source, through this material of heat exchanger heats.In separator column 60, hydrocarbons after the diasphaltene and separated from solvent, the solvent of evaporation leaves by pipeline 64.Hydrocarbons after the diasphaltene leaves separator column 60 by pipeline 62 and enters second separator column 70.From the low-quality steam of pipeline 54 be used for after the diasphaltene in the heating and separating post 70 hydrocarbons and can be used to the stripping diasphaltene after hydrocarbons in solvent.The solvent of evaporation leaves by pipeline 74.Hydrocarbons after the diasphaltene leaves by pipeline 72, is as other local product, as the raw material as catalytic cracking.Solvent vapo(u)r in the pipeline 64 and 74 enters solvent condenser/pump/separator 80, and solvent vapo(u)r becomes compressed liquid therein.Solvent leaves solvent condenser/pump 80 by pipeline 82 and enters bituminous matter extractor 20.Isolating water is removed by pipeline 84.
Fig. 2 is another embodiment of the invention.The hydrocarbons of asphaltenes enters decompression separation chamber (10) by pipeline 12.Light oil separates from the hydrocarbons of asphaltenes and discharges from decompression separation chamber (10) by pipeline 14.The hydrocarbons of asphaltenes leaves the decompression separation chamber, enters bituminous matter extractor (20) by pipeline 16.Solvent enters bituminous matter extractor (20) by pipeline 82 from solvent condenser (80).Hydrocarbons after bituminous matter and some diasphaltenes leaves bituminous matter extractor (20) by pipeline 22.Optionally be, this logistics in the pipeline 22 is separable with the recovery solvent, but this step is not shown in the drawings.Logistics in the pipeline 22 enters gasification zone (30), and it mixes with the oxygen-containing gas that imports by pipeline 32 there.The very hot synthetic gas that the partial oxidation that carry out gasification zone (30) produces leaves the gasification zone by pipeline 34.Part cooling gas and the water quench system of removing particle do not illustrate.The synthetic air of heat is through heat exchanger (40), and wherein the water in the pipeline 42 is transformed into high-quality steam in the pipeline 44.This steam is to be used in other local product.Synthetic gas leaves heat exchanger (40) by pipeline 46 then, enters second heat exchanger (50).The synthetic air of heat is through heat exchanger (50), and wherein the water in the pipeline 52 is transformed into low-quality steam in the pipeline 54.Synthetic gas leaves heat exchanger (50) then, is sent to separator column (60).Also enter separator column (60) from the hydrocarbons after the diasphaltene of bituminous matter extractor (20) by pipeline 24.In separator column (60), the hydrocarbons after the heating diasphaltene, the solvent of evaporation leaves by pipeline 64.Synthetic gas is to be used in other local product.Hydrocarbons after the diasphaltene leaves separator column (60) by pipeline 62 and enters second separator column (70).Be used for hydrocarbons after the diasphaltene in the heating and separating post (70) from the low-quality steam of pipeline 54.The solvent of evaporation leaves by pipeline 74.Hydrocarbons after the diasphaltene leaves by pipeline 72, is as other local product.Solvent vapo(u)r in the pipeline 64 and 74 enters solvent condenser/pump (80), and solvent becomes compressed liquid therein.Solvent leaves solvent condenser/pump (80) by pipeline 82, enters bituminous matter extractor (20).
Claims (17)
1, a kind of bitum technology that gasifies in the gasification zone, it comprises:
A) solvent is mixed with the hydrocarbons of asphaltenes, so that at least a portion asphaltene precipitation, therefore generate hydrocarbons and precipitated asphalt matter after the diasphaltene;
B) hydrocarbons after at least a portion diasphaltene is separated with precipitated asphalt matter and the hydrocarbons after the diasphaltene is supplied with separator column;
C) at least a portion precipitated asphalt matter is supplied with the gasification zone;
D) the gasification bituminous matter is to form synthetic gas; With
E) use from the solvent in the hydrocarbons after the sensible heat separation diasphaltene of synthetic gas.
2, the technology of claim 1, solvent wherein contains propane, butane, pentane, hexane, heptane or its mixture.
3, the technology of claim 2, solvent wherein contain the propane of 80wt% at least, butane, pentane or its mixture.
4, the technology of claim 2, solvent wherein contain propane and the butane of 80wt% at least.
5, the technology of claim 1 also is included in and utilizes the solvent producing steam in previous existence in the hydrocarbons after the remaining sensible heat separation diasphaltene in the synthetic gas.
6, the technology of claim 5 is pressed and low-pressure steam in wherein producing.
7, the technology of claim 6, wherein at least a portion low-pressure steam is used for separating the solvent in the hydrocarbons after the diasphaltene.
8, the technology of claim 1, wherein the hydrocarbons at least about the asphaltenes of 20wt% is precipitated as bituminous matter.
9, the technology of claim 1 is wherein removed from precipitated asphalt matter at least about the hydrocarbons after the diasphaltene of 90wt% in the step (b).
10, the technology of claim 1 also comprises other hydrocarbonaceous material is added in the gasification zone.
11, the technology of claim 1 is wherein carried out the separating under reduced pressure of hydrocarbons after at least a portion solvent and the diasphaltene.
12, the technology of claim 7, wherein stripping solvent the material of at least a portion steam after diasphaltene.
13, the technology of claim 1 comprises that also the sensible heat that utilizes synthetic gas makes solvent separate with bituminous matter.
14, the technology of claim 13, wherein at least a portion solvent is removed from bituminous matter by stripping.
15, the technology of claim 1 also comprises isolating solvent in the hydrocarbons after the diasphaltene that utilizes again from step (a).
16, the technology of claim 13 also comprises again and utilizing and the isolating solvent of bituminous matter.
17, the technology of claim 13 also is included in and makes solvent precipitated asphalt matter is heated to about 170 ℃ to about 260 ℃ before separating with bituminous matter, and wherein precipitated asphalt matter is as pumpable fluid supply gasification zone.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US9449498P | 1998-07-29 | 1998-07-29 | |
| US60/094,494 | 1998-07-29 | ||
| US10311898P | 1998-10-05 | 1998-10-05 | |
| US60/103,118 | 1998-10-05 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1330696A true CN1330696A (en) | 2002-01-09 |
| CN1163572C CN1163572C (en) | 2004-08-25 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB998105422A Expired - Lifetime CN1163572C (en) | 1998-07-29 | 1999-07-27 | Integration of solvent deasphalting and gasification |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US6241874B1 (en) |
| EP (1) | EP1114126B1 (en) |
| CN (1) | CN1163572C (en) |
| AR (1) | AR019954A1 (en) |
| AT (1) | ATE277146T1 (en) |
| AU (1) | AU758226B2 (en) |
| BR (1) | BR9913347A (en) |
| CA (1) | CA2338980C (en) |
| DE (1) | DE69920489T2 (en) |
| ES (1) | ES2229752T3 (en) |
| WO (1) | WO2000006670A1 (en) |
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| CN103450938A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气股份有限公司 | Inferior heavy oil processing combined process for emission reduction of carbon dioxide |
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- 1999-07-27 US US09/361,953 patent/US6241874B1/en not_active Expired - Fee Related
- 1999-07-27 DE DE69920489T patent/DE69920489T2/en not_active Expired - Lifetime
- 1999-07-27 AU AU52324/99A patent/AU758226B2/en not_active Ceased
- 1999-07-27 EP EP99937506A patent/EP1114126B1/en not_active Expired - Lifetime
- 1999-07-27 ES ES99937506T patent/ES2229752T3/en not_active Expired - Lifetime
- 1999-07-27 CN CNB998105422A patent/CN1163572C/en not_active Expired - Lifetime
- 1999-07-27 WO PCT/US1999/016922 patent/WO2000006670A1/en active IP Right Grant
- 1999-07-27 CA CA2338980A patent/CA2338980C/en not_active Expired - Lifetime
- 1999-07-27 BR BR9913347-4A patent/BR9913347A/en not_active IP Right Cessation
- 1999-07-27 AT AT99937506T patent/ATE277146T1/en not_active IP Right Cessation
- 1999-07-28 AR ARP990103745A patent/AR019954A1/en not_active Application Discontinuation
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1295141C (en) * | 2004-04-29 | 2007-01-17 | 中国石化镇海炼油化工股份有限公司 | Method for producing synthetic gas by gasifying super-heavy inferior oil mixture |
| CN103450938A (en) * | 2012-06-01 | 2013-12-18 | 中国石油天然气股份有限公司 | Inferior heavy oil processing combined process for emission reduction of carbon dioxide |
| CN103450938B (en) * | 2012-06-01 | 2016-03-09 | 中国石油天然气股份有限公司 | A kind of inferior heavy oil processing combined technical method of reducing emission of carbon dioxide |
| CN103231428A (en) * | 2013-04-12 | 2013-08-07 | 绥中未名合一再生材料科技有限公司 | Asphalt removal method for waste sleeper |
| CN108473882A (en) * | 2015-12-28 | 2018-08-31 | 埃克森美孚研究工程公司 | Integrated residual oil depitching and gasification |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2338980C (en) | 2010-04-27 |
| ATE277146T1 (en) | 2004-10-15 |
| CA2338980A1 (en) | 2000-02-10 |
| AU758226B2 (en) | 2003-03-20 |
| BR9913347A (en) | 2002-03-05 |
| DE69920489T2 (en) | 2005-12-01 |
| DE69920489D1 (en) | 2004-10-28 |
| WO2000006670A1 (en) | 2000-02-10 |
| AU5232499A (en) | 2000-02-21 |
| ES2229752T3 (en) | 2005-04-16 |
| EP1114126B1 (en) | 2004-09-22 |
| CN1163572C (en) | 2004-08-25 |
| AR019954A1 (en) | 2002-03-27 |
| US6241874B1 (en) | 2001-06-05 |
| EP1114126A1 (en) | 2001-07-11 |
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